CN107400539B - Low-temperature gasification device for low-rank fuel based on spiral pyrolyzer and fluidized bed gasifier - Google Patents
Low-temperature gasification device for low-rank fuel based on spiral pyrolyzer and fluidized bed gasifier Download PDFInfo
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- CN107400539B CN107400539B CN201710813279.9A CN201710813279A CN107400539B CN 107400539 B CN107400539 B CN 107400539B CN 201710813279 A CN201710813279 A CN 201710813279A CN 107400539 B CN107400539 B CN 107400539B
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/58—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels combined with pre-distillation of the fuel
- C10J3/60—Processes
- C10J3/64—Processes with decomposition of the distillation products
- C10J3/66—Processes with decomposition of the distillation products by introducing them into the gasification zone
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/46—Gasification of granular or pulverulent flues in suspension
- C10J3/54—Gasification of granular or pulverulent fuels by the Winkler technique, i.e. by fluidisation
- C10J3/56—Apparatus; Plants
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J3/00—Production of combustible gases containing carbon monoxide from solid carbonaceous fuels
- C10J3/72—Other features
- C10J3/82—Gas withdrawal means
- C10J3/84—Gas withdrawal means with means for removing dust or tar from the gas
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2200/00—Details of gasification apparatus
- C10J2200/15—Details of feeding means
- C10J2200/154—Pushing devices, e.g. pistons
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- C—CHEMISTRY; METALLURGY
- C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
- C10J—PRODUCTION OF PRODUCER GAS, WATER-GAS, SYNTHESIS GAS FROM SOLID CARBONACEOUS MATERIAL, OR MIXTURES CONTAINING THESE GASES; CARBURETTING AIR OR OTHER GASES
- C10J2300/00—Details of gasification processes
- C10J2300/18—Details of the gasification process, e.g. loops, autothermal operation
- C10J2300/1807—Recycle loops, e.g. gas, solids, heating medium, water
Abstract
Low-temperature gasification device for low-order fuel based on spiral pyrolyzer and fluidized bed gasifier belongs to the field of gasification of low-order fuel. A power output shaft of a motor I is in transmission connection with a power input shaft of a gear transmission case, a primary spiral pyrolyzer and an air seal machine are mutually coupled through the gear transmission case, spiral shafts of the primary and secondary spiral pyrolyzers are connected through a coupler, and the secondary spiral pyrolyzer is communicated with a fluidized bed gasifier; the upper part of the second-stage spiral pyrolyzer is provided with a water vapor inlet; the fluidized bed gasifier is communicated with the cyclone separator, the fluidized bed gasifier is communicated with the air inlet system, and the slag discharge pipe is communicated with the bottom of the fluidized bed gasifier; the cyclone separator is communicated with a primary feed back pipe, the primary feed back pipe is communicated with the spiral feed back device, the spiral feed back device is communicated with a secondary feed back pipe, and the secondary feed back pipe is communicated with the secondary spiral pyrolyzer. The invention utilizes the pyrolysis coke in-situ catalytic cracking to catalyze the low-temperature gasification of the coal coke by absorbing alkali metal and alkaline earth metal again, thereby realizing the high-efficiency low-temperature gasification of low-order fuel.
Description
Technical Field
The invention relates to a low-temperature gasification device for low-order fuel based on a spiral pyrolyzer and a fluidized bed gasifier, belonging to the field of gasification of low-order fuel.
Background
Gasification refers to the conversion of solid fuels into fuels containing CO and H by taking carbonaceous fuels (coal, coal coke or biomass, etc.) as raw materials and taking oxygen (air, oxygen-enriched oxygen or industrial pure oxygen), water vapor, carbon dioxide, etc. as gasifying agents and carrying out a series of chemical reactions at a certain temperature and pressure in specific equipment2、CH4And waiting for combustible gas.
The low-rank fuel (low-rank coal, biomass and kitchen garbage) has rich reserves and sources, low metamorphic grade, high volatile components and high gasification activity. In addition, the alkali metals and alkaline earth metals (low-rank coal is rich in sodium, calcium and magnesium, biomass is rich in potassium, calcium and magnesium, and kitchen garbage mainly contains sodium) rich in the low-rank fuel have a good catalytic effect on gasification, and the gasification rate of the fuel can be remarkably improved. Thermodynamic calculations on low-rank fuels (low-rank coal and biomass) show that when the reaction temperature is higher than 700 ℃, the energy provided is sufficient to ensure complete gasification of the fuel.
Gasification of low-rank fuels generally involves two processes, pyrolysis of the feedstock and gasification of the char. The conventional gasification process has two key problems, namely, the content of tar in the synthesis gas is high, the tar is easy to condense at low temperature (200 ℃), and is bonded with water, coke and the like to block an air supply pipeline, so that the gasification equipment is difficult to operate, and meanwhile, the energy (5-15%) contained in the tar is not effectively utilized, wherein the tar is mainly derived from the pyrolysis process of low-grade fuel; secondly, the gasification rate of the coke is low, 20-70% of alkali metal and alkaline earth metal in the low-order fuel in the pyrolysis process are released into a gas phase in the form of atoms or compounds, so that the content of a catalyst in the generated coke is reduced, the reactivity and the gasification rate are greatly reduced, and the improvement of the carbon conversion rate and the large-scale gasification equipment are not facilitated.
The two-stage pyrolysis gasification technology separates the pyrolysis of fuel and the gasification process of coke, and performs stage control to promote the decomposition of tar and improve the gasification rate of the coke. Among them, the two-stage gasification technology combining an external heating type spiral pyrolyzer and a downdraft fixed bed gasifier developed by the university of Denmark science and technology is more typical. The tar-containing pyrolysis gas generated by biomass pyrolysis and high-temperature semicoke enter a downdraft gasifier together, and when the pyrolysis gas passes through a high-temperature semicoke gasification layer, tar in the pyrolysis gas is removed, but the pyrolysis gas is limited by an external heating spiral pyrolyzer and is not easy to amplify, and the downdraft fixed bed gasifier has larger resistance and lower gasification rate. Chinese patent 94190559.4 discloses a two-stage gasification process for low-rank coal by coupling a fluidized bed pyrolyzer and an updraft fixed bed gasifier. Semicoke generated in the fluidized bed pyrolysis process (400-700 ℃ and less than 50 atm) is sent into an updraft type fixed bed for gasification (less than 1200 ℃ and less than 50 atm), pyrolysis gas and gasification gas are respectively discharged and are sent to a terminal power generation device after being mixed, but the tar content in the mixed gas is higher. Chinese patent CN101440307A discloses a two-stage gasification process coupling an updraft fixed bed gasification furnace and a fluidized bed gasification furnace, which utilizes the high temperature in the lower fluidized bed gasification furnace to further crack the tar in the upper fixed bed gasification furnace to generate the tar in the coal gas. Chinese patent CN1916123 discloses a two-stage gasification process coupling a fluidized bed and a downdraft fixed bed, which effectively reduces the tar content through the catalytic reforming action of a semicoke bed layer. Chinese patent CN102703131 discloses a two-stage gasification method for a combined fluidized bed pyrolyzer and entrained flow gasifier, which utilizes the catalytic reforming effects of high-temperature pyrolysis, partial oxidation and semicoke in an entrained flow to remove tar. Domestic patents adopt an autothermal fluidized bed or a fixed bed in the pyrolysis stage, which is beneficial to the amplification treatment of equipment.
However, in the tar removal aspect, the tar is removed only in the gasification stage by the catalytic cracking of the high-temperature coke on the tar or the high-temperature cracking of the tar, the gasification temperature is high, and the tar removal in the pyrolysis stage is not considered; higher gasification temperatures necessarily result in lower cold gasification efficiency (cold gas efficiency for coal) which decreases by about 20% as the gasification temperature increases from 900 ℃ to 1600 ℃. In the aspect of coke gasification, the prior patent improves the gasification rate by means of increasing the temperature or pressure, and the utilization of alkali metal and alkaline earth metal catalysts in low-grade fuel is insufficient; higher gasification temperatures and pressures also result in higher capital and operating costs.
Therefore, the gasification of the low-rank fuel can reduce the tar content in the synthesis gas while reducing the gasification temperature, and the alkali metal and the alkaline earth metal released in the pyrolysis process are absorbed into the coke again, so that the problems in the gasification process of the low-rank fuel can be effectively solved.
Disclosure of Invention
The invention aims to reduce the tar content in low-grade fuel synthesis gas and improve the reactivity of coke, and provides a low-grade fuel low-temperature gasification device based on a spiral pyrolyzer and a fluidized bed gasifier.
In order to solve the problems in the low-order fuel gasification, the invention adopts a spiral pyrolyzer without introducing carrier gas in the pyrolysis stage based on the existing two-stage gasification technology; in the gasification stage, a fluidized bed reactor is adopted, and the circulating material (heat carrier) is heated to supply heat to the spiral pyrolyzer while gasification is carried out.
In the invention, the low-order fuel is in a stacking state in the two-stage spiral pyrolyzer, and no carrier gas is introduced into the two-stage spiral pyrolyzer; the low-order fuel is heated by mixing with a heat carrier to be decomposed, and the pyrolysis gas overflows a fuel bed by slow diffusion; the generated pyrolysis gas and coke are directly sent into the fluidized bed gasifier to react with gasification media to release heat, and the heat carrier is heated while the pyrolysis gas and the coke are converted into gasification gas. By inhibiting the gas flow in the fuel bed layer, on one hand, the invention prolongs the retention time of tar in the fuel bed layer, so that the tar can be fully cracked under the catalytic action of coke, and the tar content in pyrolysis gas is reduced; on the other hand, the alkali metal and the alkaline earth metal released by pyrolysis in the particles are not easily carried out of the fuel bed layer due to the inhibition of gas flow, and can be adsorbed again under the action of adjacent particles for catalyzing the low-temperature gasification of coke. The close contact between the particles in the packed state enhances the effect of the above two aspects.
The purpose of the invention is realized by the following technical scheme:
the low-temperature gasification device for the low-rank fuel based on the spiral pyrolyzer and the fluidized bed gasifier comprises a material storage system, a spiral pyrolysis system, a fluidized bed gasification system and a cyclone separation system;
the material storage system comprises a material bin, an air seal machine, a gear transmission case and a first motor, the spiral pyrolysis system comprises a first-stage spiral pyrolyzer, a coupler and a second-stage spiral pyrolyzer, the fluidized bed gasification system comprises a fluidized bed gasifier, an air inlet system and a slag discharge pipe, and the cyclone separation system comprises a spiral material return device, a second-stage material return pipe, at least one cyclone separator and at least one first-stage material return pipe;
the air seal machine is arranged at the lower part in the bin, a power output shaft of the motor I is in transmission connection with a power input shaft of a gear transmission box, the gear transmission box is provided with two power output shafts, one power output shaft of the gear transmission box is in transmission connection with the air seal machine, the other power output shaft of the gear transmission box is in transmission connection with a spiral shaft of the primary spiral pyrolyzer, and a fuel outlet at the lower end of the bin is communicated with a fuel inlet at the upper end of the primary spiral pyrolyzer;
the screw shaft of the primary screw pyrolyzer is connected with the screw shaft of the secondary screw pyrolyzer through a coupler, an external cylinder of the primary screw pyrolyzer is butted with an external cylinder of the secondary screw pyrolyzer, and a pyrolysis product outlet of the secondary screw pyrolyzer is communicated with the fluidized bed gasifier; the spiral pyrolysis system is obliquely arranged, one end of a fuel inlet of the primary spiral pyrolyzer is lower than one end of a pyrolysis product outlet of the secondary spiral pyrolyzer, and a water vapor inlet is formed in the upper part of the secondary spiral pyrolyzer;
the top of the fluidized bed gasifier is communicated with the cyclone separator, the bottom of the fluidized bed gasifier is communicated with the air inlet system, and one end of the slag discharge pipe is communicated with the bottom of the fluidized bed gasifier;
the cyclone separator is characterized in that a primary material return pipe is correspondingly communicated with the bottom of the cyclone separator, the lower parts of all the primary material return pipes are communicated with the upper part of the spiral material return device, the lower part of the spiral material return device is communicated with the upper part of the secondary material return pipe, the secondary material return pipe is arranged at the junction of the primary spiral pyrolyzer and the secondary spiral pyrolyzer, and the lower part of the secondary material return pipe is communicated with a circulating material return inlet at the upper part of the secondary spiral pyrolyzer.
Compared with the prior art, the invention has the beneficial effects that:
1. the tar content in the synthesis gas is low, and the synthesis gas can be used without purification (or simple purification). The device disclosed by the invention reduces the content of tar in two stages, firstly, in the spiral pyrolyzer, volatile matters can only enter a fluidized bed gasification system through slow diffusion due to no carrier gas, and the diffusion is carried out in a coke layer, so that the catalytic cracking of the tar generated by pyrolysis is facilitated; secondly, in the fluidized bed gasifier, the residual tar reacts with the oxygen-containing water vapor to realize complete conversion.
2. Higher carbon conversion and cold gasification efficiency. The device can enrich the catalysts such as alkali metal, alkaline earth metal and the like in the low-order fuel in the coke and is used for catalyzing the gasification reaction of the coke; the coke with high reactivity directly enters the fluidized bed gasifier without being cooled to participate in gasification reaction, and the high activity of the in-situ coke is reserved. The overall gasification temperature is lower (less than 1000 ℃), and higher cold gasification efficiency is ensured.
3. The pyrolysis process is controllable, and the consistency of pyrolysis products is good. According to the device disclosed by the invention, the retention time and the temperature of the low-order fuel in the spiral pyrolyzer are adjustable, the pyrolysis process is controllable, the consistency of pyrolysis product components is good, and the later-stage gasification condition can be favorably set.
4. Wide raw material source, strong applicability and good economical efficiency. The invention can be widely applied to low-grade fuels because low-grade coal, biomass and kitchen garbage all contain abundant alkali metals and alkaline earth metals and can be used for catalyzing gasification reaction of the low-grade fuels. The low-order fuel is low in price, the moisture existing in the low-order fuel can be utilized in situ, the low-order fuel does not need to be dried in advance, and the utilization economy of the low-order fuel is effectively improved.
5. The oxygen consumption is low. The lower gasification temperature effectively reduces the consumption of oxygen; thus gasifying the medium or using oxygen-enriched gas to reduce N in the synthesis gas2The concentration of (c).
Drawings
FIG. 1 is a schematic structural diagram I of a low-temperature gasification device of low-rank fuel based on a spiral pyrolyzer and a fluidized bed gasifier.
FIG. 2 is a structural schematic diagram of a low-temperature gasification device of low-rank fuel based on a spiral pyrolyzer and a fluidized bed gasifier, wherein synthesis gas is discharged after being released by a heat exchange system, and normal-temperature water is converted into steam and discharged after absorbing heat from the heat exchange system;
FIG. 3 is a third structural schematic diagram of a low-temperature gasification device for low-rank fuels based on a spiral pyrolyzer and a fluidized bed gasifier, wherein synthesis gas is discharged after being discharged through a dividing wall type heat exchanger and a heat exchange system in sequence, and normal-temperature water is converted into steam to be discharged after absorbing heat from the heat exchange system;
fig. 4 is a schematic diagram of a gear box.
The names and labels of the components in fig. 1-4 are as follows:
the device comprises a material storage system 1, a material bin 11, an air seal machine 12, a gear transmission case 13, a driving gear I13-1, a driving gear II 13-2, a driven gear I13-3, a driven gear II 13-4, a power input shaft 13-5, a power output shaft 13-6, a motor I14, a spiral pyrolysis system 2, a primary spiral pyrolyzer 21, a coupler 22, a secondary spiral pyrolyzer 23, a steam inlet 23-1, a dividing wall type heat exchanger 24, a fluidized bed gasification system 3, a fluidized bed gasifier 31, an air inlet system 32, a slag discharge pipe 33, a cyclone separation system 4, a cyclone separator 41, a primary return pipe 42, a spiral return pipe 43, a secondary return pipe 44, a motor II 45 and a heat exchange system 5.
Wherein: the airlock 12, the gear transmission case 13, the first motor 14, the first-stage spiral pyrolyzer 21, the coupling 22, the second-stage spiral pyrolyzer 23, the dividing wall type heat exchanger 24, the fluidized bed gasifier 31, the second motor 45, the spiral material returning device 43 and the heat exchange system 5 are all in the prior art and are outsourced products.
Detailed Description
The technical solution of the present invention is further described below with reference to the accompanying drawings, but not limited thereto, and any modification or equivalent replacement of the technical solution of the present invention without departing from the spirit and scope of the technical solution of the present invention shall be covered by the protection scope of the present invention.
The first embodiment is as follows: as shown in fig. 1 and fig. 4, the embodiment discloses a low-temperature gasification device for low-rank fuel based on a spiral pyrolyzer and a fluidized bed gasifier, which comprises a material storage system 1, a spiral pyrolysis system 2, a fluidized bed gasification system 3 and a cyclone separation system 4;
the material storage system 1 comprises a material bin 11, an air seal machine 12, a gear transmission case 13 and a motor 14, the spiral pyrolysis system 2 comprises a primary spiral pyrolyzer 21, a coupler 22 and a secondary spiral pyrolyzer 23, the fluidized bed gasification system 3 comprises a fluidized bed gasifier 31, an air inlet system 32 and a slag discharge pipe 33, and the cyclone separation system 4 comprises a spiral material return 43, a secondary material return pipe 44, at least one cyclone separator 41 and at least one primary material return pipe 42;
the airlock 12 is arranged at the lower part in the stock bin 11, a power output shaft of the motor I14 is in transmission connection with a power input shaft of a gear transmission box 13, the gear transmission box 13 is provided with two power output shafts 13-6, one power output shaft 13-6 of the gear transmission box 13 is in transmission connection with the airlock 12, the other power output shaft 13-6 of the gear transmission box 13 is in transmission connection with a spiral shaft of the primary spiral pyrolyzer 21, and a fuel outlet at the lower end of the stock bin 11 is communicated with a fuel inlet at the upper end of the primary spiral pyrolyzer 21;
the screw shaft of the primary screw pyrolyzer 21 is connected with the screw shaft of the secondary screw pyrolyzer 23 through a coupler 22, the external cylinder of the primary screw pyrolyzer 21 is butted with the external cylinder of the secondary screw pyrolyzer 23, and the pyrolysis product outlet of the secondary screw pyrolyzer 23 is communicated with the fluidized bed gasifier 31; the spiral pyrolysis system 2 is obliquely arranged, one end of a fuel inlet of the primary spiral pyrolyzer 21 is lower than one end of a pyrolysis product outlet of the secondary spiral pyrolyzer 23, and a water vapor inlet 23-1 is formed in the upper part of the secondary spiral pyrolyzer 23;
the top of the fluidized bed gasifier 31 is communicated with the cyclone separator 41, the bottom of the fluidized bed gasifier 31 is communicated with the air inlet system 32, and one end of the slag discharge pipe 33 is communicated with the bottom of the fluidized bed gasifier 31;
the bottom of the cyclone separator 41 is correspondingly communicated with a first-stage return pipe 42, the lower parts of all the first-stage return pipes 42 are communicated with the upper part of a spiral return material device 43, the lower part of the spiral return material device 43 is communicated with the upper part of a second-stage return pipe 44, the second-stage return pipe 44 is arranged at the junction of the first-stage spiral pyrolyzer 21 and the second-stage spiral pyrolyzer 22, and the lower part of the second-stage return pipe 44 is communicated with a circulating return material (heat carrier) inlet at the upper part of the second-stage spiral pyrolyzer 22.
In this embodiment, the primary screw pyrolyzer 21 and the airlock 12 are coupled to each other by means of a gear box 13 to ensure continuous feeding of the low-rank fuel.
The gear transmission 13 in the embodiment comprises a driving gear I13-1, a driving gear II 13-2, a driven gear I13-3, a driven gear II 13-4, a power input shaft 13-5 and two power output shafts 13-6; the driving gear I13-1 and the driving gear II 13-2 share one power input shaft 13-5, the driving gear I13-1 is meshed with a driven gear I13-3, the driving gear II 13-2 is meshed with a driven gear II 13-4, the driven gear I13-3 is installed on one power output shaft 13-6, and the driven gear II 13-4 is installed on the other power output shaft 13-6.
The screw shaft of the screw material returning device 43 in the present embodiment is driven to rotate by a second motor 45.
Second embodiment as shown in fig. 1, the second embodiment is further described with respect to the first embodiment, and the included angle between the bottom surface of the spiral pyrolysis system 2 and the horizontal plane is α =5 ° -45 °, so as to ensure the fullness of the pyrolysis products in the spiral pyrolyzer, and the volatile matter can only diffuse out through the solid product layer, thereby fully reacting with the solid product layer.
The third concrete implementation mode: as shown in fig. 1, the present embodiment is further described with respect to the first embodiment, the length of the spiral pyrolysis system 2 is set to L, the starting position of the length of the spiral pyrolysis system 2 is located at the fuel inlet end of the primary spiral pyrolyzer 21, and the abutting position of the outer cylinder of the primary spiral pyrolyzer 21 and the outer cylinder of the secondary spiral pyrolyzer 23 is located in the 1/3L region in the length direction of the spiral pyrolysis system 2. Ensuring that the heat carrier and the fed low-rank fuel are in sufficient contact and heat transfer in the secondary spiral pyrolyzer 23.
The fourth concrete implementation mode: as shown in FIG. 1, this embodiment is further described with respect to the third embodiment, wherein the water vapor inlet 23-1 is disposed adjacent to the fuel inlet.
The method is used for supplementing the deficiency of moisture (including moisture released in the drying and pyrolysis processes) in the gas phase, so that the gasification of the coke and the reformation of the tar under the condition are maximized, the content of the tar at the outlet of a pyrolysis product is reduced, the particle size and the quality of the coke are reduced, and the method is favorable for the complete conversion of the tar and the coke in the later period.
The fifth concrete implementation mode: as shown in fig. 1, the first or third embodiment is further described, and the material conveying amount of the second-stage spiral pyrolyzer 23 is 2-5 times of the material conveying amount of the first-stage spiral pyrolyzer 21.
The sixth specific implementation mode: as shown in fig. 2, the present embodiment is further described with respect to the first embodiment, and the low-temperature gasification apparatus for low-rank fuel based on spiral pyrolyzer and fluidized-bed gasifier further includes a heat exchanger system 5; the synthesis gas inlet of the heat exchanger system 5 is communicated with the synthesis gas outlet of the cyclone separation system 4 through a pipeline (the water vapor generated by the heat exchanger system 5 is respectively introduced into the secondary spiral pyrolyzer 23 and the fluidized bed gasifier 31 according to a certain proportion).
The seventh embodiment: as shown in fig. 3, the present embodiment is further explained for the sixth embodiment, and the low-temperature gasification apparatus for low-rank fuel based on the spiral pyrolyzer and the fluidized bed gasifier further includes a dividing wall type heat exchanger 24; the dividing wall type heat exchanger 24 is arranged at the outer side of the spiral pyrolysis system 2, and the two ends of the dividing wall type heat exchanger 24 are respectively communicated with a synthetic gas outlet of the cyclone separation system 4 and a synthetic gas inlet of the heat exchange system 5.
The dwell time of low order fuel in spiral pyrolysis system 2 is controlled by its inclination and rotational speed, and the temperature is then controlled by the quantity of heat carrier, and above both make the pyrolysis process of low order fuel controllable, and the component of pyrolysis product is unanimous, and the complete conversion of tar and coke is guaranteed in the setting of the later stage gasification condition of being convenient for.
The pyrolyzed coke and pyrolysis gas containing a small amount of tar directly enter the fluidized bed gasifier 31 for gasification, the gasification medium is oxygen-containing gas and water vapor, and the temperature in the fluidized bed gasifier 31 is controlled by adjusting the oxygen content. Because the coke is not cooled, the negative influence of a cold quenching effect is avoided, and the high reactivity of the in-situ coke is kept; more importantly, the coke is greatly enriched in alkali metals and alkaline earth metals to catalyze the gasification process of the coke, and the alkali metals and the alkaline earth metals jointly ensure that the coke and the alkaline earth metals can be used for ensuring the gasification process of the cokeLow temperature gasification activity of coke. The gas generated in the fluidized-bed gasifier 31 is mainly composed of H2、CO、CO2And CH4。
The circulating material (heat carrier) with the temperature of 800-1000 ℃ at the outlet of the fluidized bed gasifier 31 is separated by the cyclone separation system 4 and then enters the spiral pyrolysis system 2, and then is heated by mixing with low-order fuel.
In the low-temperature gasification device, a heat exchange system 5 is arranged at the downstream of the synthesis gas, and the water vapor generated by the heat exchange system 5 is respectively introduced into the secondary spiral pyrolyzer 23 and the fluidized bed gasifier 31 according to a certain proportion. Sensible heat in the synthesis gas is used for generating steam required by the heat exchange system 5, and the overall gasification efficiency of the heat exchange system 5 is improved.
According to the low-temperature gasification device, the dividing wall type heat exchanger 24 is further arranged outside the spiral pyrolysis system 2, a primary synthesis gas inlet and a secondary synthesis gas outlet are respectively arranged at two ends of the dividing wall type heat exchanger 24, the primary synthesis gas outlet of the cyclone separation system 4 is communicated with the primary synthesis gas inlet of the dividing wall type heat exchanger 24 through a pipeline, and the secondary synthesis gas outlet of the dividing wall type heat exchanger 24 is communicated with the secondary synthesis gas inlet of the heat exchange system 5. Sensible heat in the synthesis gas is respectively used for supplying heat to the pyrolysis reaction process and generating steam required by the heat exchange system 5, so that the cascade utilization of energy is realized, and the overall gasification efficiency of the heat exchange system 5 is further improved.
The working process of the invention is as follows: the airlock 12 and the primary screw pyrolyzer 21 are coupled to each other via a gear box 13 to continuously feed low-rank fuel into the screw pyrolysis system 2. The low-grade fuel is mixed with a circulating return material (heat carrier) with the temperature of 800-1000 ℃ to carry out temperature rise drying and pyrolysis, including gasification and reforming of partial high-reactivity pyrolysis products. Part of the water vapor required by gasification and reforming is derived from the moisture generated by drying and pyrolysis of the low-order fuel, the other part of the water vapor is derived from the moisture supplemented through a water vapor inlet 23-1 on the spiral pyrolysis system 2, the low-order fuel or coke is conveyed into the fluidized bed gasifier 31 through the rotation of a spiral shaft (auger) in the spiral pyrolysis system 2, and the volatile matter is conveyed into the fluidized bed gasifier 31 through diffusion. The pyrolysis products (residual tar and char) are reformed and gasified inside the fluidized-bed gasifier 31, and the temperature inside the fluidized-bed gasifier 31 is controlled by adjusting the portion of the oxygen-containing gas. The heat carrier and the synthesis gas at the outlet of the fluidized bed gasifier 31 are separated by the cyclone 4, the heat carrier enters the spiral pyrolysis system 2, and the synthesis gas enters other downstream processing equipment.
One end of a fuel inlet of the spiral pyrolysis system 2 is lower than one end of a pyrolysis product outlet, so that the fullness degree of coke in the spiral pyrolysis system 2 is increased (the fullness degree can be adjusted by changing an included angle between the bottom surface of the spiral pyrolysis system 2 and a horizontal plane), volatile matters are enabled to enter the fluidized bed gasifier 31 after passing through a coke bed, and catalytic cracking of tar in the volatile matters by the coke is facilitated; meanwhile, as no carrier gas is introduced, the volatile matters must enter the fluidized bed gasifier 31 through diffusion, so that the retention time of the volatile matters in the coke bed layer is increased, and the catalytic cracking reaction of the volatile matters is promoted. In addition, the increase of the fullness of the coke and the introduction of no carrier gas are beneficial to the reabsorption of the alkali metal and the alkaline earth metal released by pyrolysis, and the large volatilization of the alkali metal and the alkaline earth metal in the coke in the pyrolysis process is inhibited, so that most of the alkali metal and the alkaline earth metal are enriched on coke particles.
The invention is provided with a heat exchange system 5 at the downstream of the synthesis gas, and the water vapor generated by the heat exchange system 5 is respectively introduced into the secondary spiral pyrolyzer 23 and the fluidized bed gasifier 31 according to a certain proportion. The synthesis gas separated by the cyclone separation system 4 is discharged after releasing heat in the heat exchange system 5, normal-temperature water is introduced into the heat exchange system 5 to be used for cooling the synthesis gas, and the heated water vapor (400-600 ℃) is utilized by the system.
The spiral pyrolysis system 2 is also externally provided with a dividing wall type heat exchanger 24, the dividing wall type heat exchanger 24 is respectively provided with a primary synthesis gas inlet and a secondary synthesis gas outlet at two ends, a primary synthesis gas outlet 41-1 of the cyclone separator 41 is communicated with the primary synthesis gas inlet of the dividing wall type heat exchanger 24 through a pipeline, and a secondary synthesis gas outlet of the dividing wall type heat exchanger 24 is communicated with the secondary synthesis gas inlet of the heat exchange system 5. The first-stage synthesis gas separated by the cyclone separation system 4 is subjected to heat release through the dividing wall type heat exchanger 24 in sequence, becomes second-stage synthesis gas, enters the heat exchange system 5 to release heat again, becomes third-stage synthesis gas and is discharged, and the heated water vapor (200-400 ℃) is utilized by the system.
Claims (6)
1. The utility model provides a low order fuel low temperature gasification equipment based on spiral pyrolyzer and fluidized bed gasifier which characterized in that: the device comprises a material storage system (1), a spiral pyrolysis system (2), a fluidized bed gasification system (3) and a cyclone separation system (4); the material storage system (1) comprises a material bin (11), an air seal machine (12), a gear transmission case (13) and a motor I (14), the spiral pyrolysis system (2) comprises a primary spiral pyrolyzer (21), a coupler (22) and a secondary spiral pyrolyzer (23), the fluidized bed gasification system (3) comprises a fluidized bed gasifier (31), an air inlet system (32) and a slag discharge pipe (33), and the cyclone separation system (4) comprises a spiral material return device (43), a secondary material return pipe (44), at least one cyclone separator (41) and at least one primary material return pipe (42);
the air seal machinery (12) is arranged at the lower part in the stock bin (11), a power output shaft of the motor I (14) is in transmission connection with a power input shaft of the gear transmission case (13), the gear transmission case (13) is provided with two power output shafts (13-6), one power output shaft (13-6) of the gear transmission case (13) is in transmission connection with the air seal machinery (12), the other power output shaft (13-6) of the gear transmission case (13) is in transmission connection with a spiral shaft of the primary spiral pyrolyzer (21), and a fuel outlet at the lower end of the stock bin (11) is communicated with a fuel inlet at the upper end of the primary spiral pyrolyzer (21);
the screw shaft of the primary screw pyrolyzer (21) is connected with the screw shaft of the secondary screw pyrolyzer (23) through a coupling (22), the external cylinder of the primary screw pyrolyzer (21) is butted with the external cylinder of the secondary screw pyrolyzer (23), and the pyrolysis product outlet of the secondary screw pyrolyzer (23) is communicated with the fluidized bed gasifier (31); the spiral pyrolysis system (2) is obliquely arranged, one end of a fuel inlet of the primary spiral pyrolyzer (21) is lower than one end of a pyrolysis product outlet of the secondary spiral pyrolyzer (23), and a water vapor inlet (23-1) is formed in the upper part of the secondary spiral pyrolyzer (23);
the top of the fluidized bed gasifier (31) is communicated with the cyclone separator (41), the bottom of the fluidized bed gasifier (31) is communicated with the air inlet system (32), and one end of the slag discharge pipe (33) is communicated with the bottom of the fluidized bed gasifier (31); the bottom of the cyclone separator (41) is correspondingly communicated with a primary feed back pipe (42), the lower parts of all the primary feed back pipes (42) are communicated with the upper part of a spiral feed back device (43), the lower parts of the spiral feed back devices (43) are communicated with the upper part of a secondary feed back pipe (44), the secondary feed back pipe (44) is arranged at the junction of the primary spiral pyrolyzer (21) and the secondary spiral pyrolyzer (22), and the lower part of the secondary feed back pipe (44) is communicated with a circulating feed back inlet at the upper part of the secondary spiral pyrolyzer (22); the circulating material at 800-1000 ℃ at the outlet of the fluidized bed gasifier (31) is separated by the cyclone separation system (4) and then enters the spiral pyrolysis system (2); the material conveying amount of the secondary spiral pyrolyzer (23) is 2-5 times of that of the primary spiral pyrolyzer (21).
2. The low-temperature gasification device for low-rank fuel based on the spiral pyrolyzer and the fluidized bed gasifier according to claim 1, wherein the included angle between the bottom surface of the spiral pyrolysis system (2) and the horizontal plane is α -5-45 °.
3. The low-rank fuel low-temperature gasification apparatus based on a spiral pyrolyzer and fluidized bed gasifier according to claim 1, characterized in that: the length of the spiral pyrolysis system (2) is set to be L, the starting position of the length of the spiral pyrolysis system (2) is located at one end of a fuel inlet of the primary spiral pyrolyzer (21), and the butt joint position of the external cylinder of the primary spiral pyrolyzer (21) and the external cylinder of the secondary spiral pyrolyzer (23) is arranged in the 1/3L area in the length direction of the spiral pyrolysis system (2).
4. The low-rank fuel low-temperature gasification apparatus based on a spiral pyrolyzer and fluidized bed gasifier according to claim 3, characterized in that: the water vapor inlet (23-1) is arranged close to the fuel inlet.
5. The low-rank fuel low-temperature gasification apparatus based on a spiral pyrolyzer and fluidized bed gasifier according to claim 1, characterized in that: the low-temperature gasification device for the low-rank fuel based on the spiral pyrolyzer and the fluidized bed gasifier also comprises a heat exchanger system (5); and a synthetic gas inlet of the heat exchanger system (5) is communicated with a synthetic gas outlet of the cyclone separation system (4) through a pipeline.
6. The low-rank fuel low-temperature gasification apparatus based on a spiral pyrolyzer and fluidized bed gasifier according to claim 5, characterized in that: the low-temperature gasification device for the low-rank fuel based on the spiral pyrolyzer and the fluidized bed gasifier also comprises a dividing wall type heat exchanger (24); the dividing wall type heat exchanger (24) is arranged at the outer side of the spiral pyrolysis system (2), and the two ends of the dividing wall type heat exchanger (24) are respectively communicated with a synthetic gas outlet of the cyclone separation system (4) and a synthetic gas inlet of the heat exchange system (5).
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| CN105602623A (en) * | 2015-12-16 | 2016-05-25 | 上海理工大学 | Two-stage down-suction biomass gasifier |
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| CN105602623A (en) * | 2015-12-16 | 2016-05-25 | 上海理工大学 | Two-stage down-suction biomass gasifier |
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